CN105314653B - Control system and control method for urea hydrolysis reactor - Google Patents
Control system and control method for urea hydrolysis reactor Download PDFInfo
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- CN105314653B CN105314653B CN201510772045.5A CN201510772045A CN105314653B CN 105314653 B CN105314653 B CN 105314653B CN 201510772045 A CN201510772045 A CN 201510772045A CN 105314653 B CN105314653 B CN 105314653B
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Abstract
The invention provides a control system and a control method for a urea hydrolysis reactor. According to the control system and method, hydrolysis reaction product gas demand mass flow and hydrolysis reaction heat demand amount can be directly obtained through ammonia gas demand amount, the adjustment is in time, the load following performance of the hydrolysis reaction speed is improved, and the ammonia gas supply is stable and efficient. The control method comprises the steps: 1, adjusting the product gas demand mass flow according to ammonia gas demand mass flow rate; 2, adjusting steam flow rate according to the ammonia gas demand amount. The control system comprises a PLC (Programmable Logic Controller) used for receiving the ammonia gas demand instruction of the hydrolysis reactor and the measurement signal of the hydrolysis reactor. Through introduction and setting of the ammonia gas demand mass flow rate, the hydrolysis reaction product gas demand mass flow rate and hydrolysis reaction heat demand amount can be directly obtained, and through in-time adjustment of an executing mechanism, the load following performance of the hydrolysis reaction speed is improved, the purpose of combined operation of a urea hydrolysis ammonia producing system and an SCR flue gas denitrification system is achieved, and continuous, stable and efficient ammonia gas supply is ensured.
Description
Technical field
The present invention relates to hydrolysis of urea technique for production of ammonia in flue gas denitrification system, specially a kind of hydrolysis of urea reactor control
System and method.
Background technology
The coal burning of coal-fired power plant is accompanied by substantial amounts of nitrogen oxides (NOX) discharge, air is polluted.With
The increasingly strict of national environmental protection policy, using ammonia (NH3) boiler emission flue gas is carried out at denitration as reducing agent
The technology of reason, has popularized in an all-round way.Now, coal-fired power plant how safety, it is continuous, effectively prepare ammonia and become numerous lifes
Produce the new problem that enterprise faces.
In actual production process, using liquefied ammonia, ammoniacal liquor prepare denitrification reducing agent ammonia, have and its strict examination ＆ approval and
Regulation Policy, and the storage device of liquefied ammonia, ammoniacal liquor belongs to major hazard source, safe operation cost is high.Hence with risk system
The relatively low urea granules of number prepare the process program of ammonia and have been increasingly becoming big fecund enterprise first-selection.
Urea granules common at present prepare the process of ammonia mainly has urea liquid pyrolysis scheme (hereinafter referred to as
" pyrolysis ") and urea liquid hydrolysis approach (hereinafter referred to as " hydrolyzing ").The ammonia spraying amount control of pyrolysis scheme can be by molten to urea
The inlet of liquid carries out simple closed-loop control, and regulation quality disclosure satisfy that unit load fluctuation and the requirement of strict environmental protection index.
But pyrolysis scheme need to configure the electric heater of relatively high power, power consumption greatly, directly influences the energy saving in running level of unit.
Hydrolysis approach is heated using low parameter water vapour to urea liquid, and rush brings it about chemical reaction, is produced also
Originality product gas, operating cost is low and security is higher.But due to there is chemical reaction in program technological process, relative to
There is sluggishness in physical change, cause the load follow of hydrolysis approach poor.Due to hydrolysis of urea reactor product gas course of conveying
In need high temperature heat tracing, otherwise easily crystallization causes pipeline blockage, therefore ensures stable vapour source using the method for installing surge tank
The scheme of pressure is relatively costly.
At present conventional scheme is to adjust hydrolysis reactor steam flow, adjusts supply gas pressure.When unit load up, lead to
Crossing increase hydrolysis reactor quantity of steam increases input heat, accelerates hydrolysis and ensures supply gas pressure.But the process has larger
Retardance, causes SCR reactors ammonia spraying amount not enough, and boiler discharged nitrous oxides short-term is exceeded.When unit load down, ammonia is needed
The amount of asking declines, and hydrolysis of urea reaction is slowed down.It is not exceeded in order to ensure hydrolysis of urea reactor pressure, spray need to be continued in flue gas
Ammonia, this will cause SCR reactor outlet the escaping of ammonia exceeded, upstream device will be impacted, while causing the waste of urea liquid.
The content of the invention
For problems of the prior art, the present invention provides one kind and can directly obtain hydrolysis by ammonia demand
Reactor product gas requirement quality flow and hydrolysis calorific requirement, adjustment is timely so that the load follow of hydrolysis speed
Improve, the hydrolysis of urea reactor control system and method for ammonia supply stability and high efficiency.
The present invention is to be achieved through the following technical solutions：
A kind of hydrolysis of urea reactor control method, comprises the steps,
Step one, is adjusted according to ammonia requirement quality flow to product gas requirement quality flow；
1.1 by urea solution density and urea solution temperature, by urea solution density and mass concentration relation function f3,
Obtain urea solution mass concentration under corresponding temperature operating mode；
1.2 by ammonia demand and urea solution mass concentration, by hydrolysis product gas requirement quality flow and ammonia
Gas requirement quality discharge relation function f1, obtain product gas requirement quality flow under correspondence urea concentration operating mode；
1.3 using product gas requirement quality flow as product throughput PID control desired value, with product gas correction factor
Closed loop product throughput PID control is together carried out with the real-time traffic of product gas, realizes that product gas requirement quality flow follows ammonia
The direct change of gas demand；
Step 2, is adjusted according to ammonia demand to steam flow；
2.1 by urea solution mass concentration and product gas requirement quality flow, by hydrolysis product gas requirement quality
Flow and reaction calorific requirement relation function f2, obtain reacting calorific requirement under correspondence urea solution mass concentration operating mode；
2.2 by vapor (steam) temperature and steam pressure, by saturated steam gasification latent heat function f4, obtain steam and be gasified totally
Current thermal discharge；And with reaction calorific requirement compare obtain heat when steam demand flow；
2.3 using steam demand flow as the desired value of steam flow PID control, steam with steam correction factor and in real time
Steam flow amount together carries out closed loop steam flow PID control, realizes that steam flow follows the direct change of ammonia demand.
Preferably, hydrolysis product gas requirement quality flow and ammonia requirement quality discharge relation function f1, concrete table
It is shown as,
QProduct gas=(QNH3×1.7647)/w；
Wherein, QProduct gasFor hydrolysis of urea reactor product demand gas mass flow；QNH3For ammonia requirement quality flow；W is urine
Plain concentration of polymer solution.
Preferably, hydrolysis product gas requirement quality flow and reaction calorific requirement relation function f2, it is embodied as,
qInhale=A × w × QProduct gas
Wherein, qInhaleCalorific requirement is reacted for hydrolysis of urea；A is that hydrolysis of urea reactor product gas requirement quality flow is needed with reaction
Heat gain coefficient；QProduct gasFor hydrolysis of urea reactor product gas requirement quality flow.
Preferably, urea solution density and mass concentration relation function f3, it is embodied as,
W=2.71 × 10-3t-4.2+(7.36×10-6t2+29.72t+26.31ρ-12.12)1/2；
Wherein, urea solution temperature when t reacts for hydrolysis of urea；ρ is urea solution density.
Preferably, by saturated steam gasification latent heat function f4；
When plus vapours be saturated mode when be expressed as,
qPut=4.184 × (- 0.003t2+0.139t+557.6)；
Wherein, qPutSaturation water is condensed into by unit quality saturated steam and releases heat；
When it is unsaturated state to add vapours, steam pressure is introduced into f4In be modified.
A kind of hydrolysis of urea reactor control system, including anti-for receiving hydrolysis reactor ammonia requirement command, hydrolysis
Answer the PLC of device measurement signal；
Described PLC is included such as lower module；
For according to urea solution density and urea solution temperature, by urea solution density and mass concentration relation function
f3, obtain the 3rd detection module of urea solution mass concentration under corresponding temperature operating mode；
For ammonia demand and urea solution mass concentration, by hydrolysis product gas requirement quality flow and ammonia
Requirement quality discharge relation function f1, obtain the first detection of product gas requirement quality flow under correspondence urea concentration operating mode
Module；
For using product gas requirement quality flow as product throughput PID control desired value, with product gas amendment system
The real-time traffic of number and product gas together carries out the product gas pid control module of closed loop product throughput PID control；Product gas
The output end connection product gas requirement quality flow control valve of pid control module；
For according to urea solution mass concentration and product gas requirement quality flow, by hydrolysis product gas demand matter
Amount flow and reaction calorific requirement relation function f2, obtain reaction calorific requirement second under correspondence urea solution mass concentration operating mode and detect
Module；
For according to vapor (steam) temperature and steam pressure, by saturated steam gasification latent heat function f4, obtain steam complete
The current thermal discharge of gasification；And with reaction calorific requirement compare obtain heat when the detection module of steam demand flow the 4th；
For using steam demand flow as steam flow PID control desired value, with steam correction factor and in real time
Steam flow together carries out the steam pid control module of closed loop steam flow PID control；The output end of steam pid control module
Connection steam flow control valve.
Compared with prior art, the present invention has following beneficial technique effect：
Introducing and setting that the present invention passes through ammonia requirement quality flow, immediately arrive at hydrolysis product gas requirement quality
Flow and hydrolysis calorific requirement, and adjusted in time by executing agency so that the load follow of hydrolysis speed is improved,
Reach the purpose of urea hydrolysis ammonia producing system and the cooperation of SCR flue gas denitrification systems, it is ensured that ammonia is continuous, stable, height
The supply of effect.
Further, urea liquid is drawn by the urea solution density that collects in hydrolysis of urea reactor, temperature
Real-time mass concentration value, for accurately calculating the operating mode under in hydrolysis of urea product gas ammonia composition, and by needing with ammonia
The contrast of the amount of asking introduces the system by deviation data is run.
Further, by the heating steam pressure that collects in hydrolysis of urea reactor, heating vapor (steam) temperature and add
Vapours mass flow, draws plus vapours thermal discharge instantaneous value, and compares with current hydrolysis of urea reaction calorific requirement, by steaming
Vapour Flow-rate adjustment eliminates the deviation, it is ensured that the system heating load can timely respond to operation demand.
Further, by the product gas requirement quality flow obtained in hydrolysis of urea reactor, by product gas demand
Product gas demand deviation introduces control system under mass flow instantaneous value and the operating mode, and by product gas requirement quality flow
Regulating valve eliminates deviation, and final response needs ammonia amount load.
Description of the drawings
Fig. 1 is the logic diagram of control method of the present invention.
Specific embodiment
With reference to specific embodiment, the present invention is described in further detail, it is described be explanation of the invention and
It is not to limit.
As shown in figure 1, the executing agency for participating in automatically controlling in the present invention is hydrolysis product gas requirement quality flow
Regulating valve and heating steam flow control valve；Participating in the measurement data of hydrolysis of urea reaction controlling includes urea liquid in reactor
Temperature, urea solution density, heating steam pressure heats vapor (steam) temperature, steam mass flow, product gas requirement quality flow；
Participating in the function of the control includes：During different urea concentration operating modes, hydrolysis product gas requirement quality flow and ammonia
Makings amount discharge relation f1；During different urea concentration operating modes, hydrolysis product gas requirement quality flow needs heat with reaction
Magnitude relation f2；During different temperatures operating mode, urea solution density and mass concentration relation f3；Saturated steam gasification latent heat calculates letter
Number f4.
When urea liquid hydrolysis ammonia system is run, the density of urea liquid, temperature in reactor are obtained according to measurement
Degree real-time status.By function f3Calculate the real-time mass concentration of aqueous solution of urea in reactor.In different urea liquids
During concentration operating mode, ammonia component is different in hydrolysis product gas.In order to avoid because it is prepared by urea liquid when concentration deviation shadow
Ring, improve the accuracy of control, urea liquid real-time mass concentration need to be introduced control system.
Meanwhile, by ammonia real-time requirement amount and the above-mentioned urea liquid real-time concentration for drawing of SCR device, by function f1
Calculate under the operating condition, the requirement quality flow of hydrolysis of urea reactor product gas.The product gas requirement quality flow
Value be a whole set of control system it is final follow desired value.
By the value and the measured value of product gas requirement quality flow, the calculating of deviation PID is carried out, and to product gas requirement quality
Flow control valve carries out closed-loop control, and the final operating load for causing hydrolysis of urea to react ammonia system processed reaches and follows SCR device
The purpose of load.
Meanwhile, being calculated using function f2 can obtain the hydrolysis of product gas requirement quality flow under the operating mode
Calorific requirement.According to heating steam pressure, vapor (steam) temperature is heated, the heat release for now adding vapours to be gasified totally is drawn by function f4
Amount.The demand of heating steam mass flow, desired value of the flow value as steam flow control valve will synchronously be drawn.The value
The calculating of deviation PID will be carried out in the measured value of heating steam mass flow, closed-loop automatic control is carried out to steam flow control valve,
Hydrolysis of urea reaction unit heating load is automatically controlled with reaching.
The present invention is drawn and needed with actual ammonia by the real-time detection to each parameter of hydrolysis of urea reactor and accurately calculating
The operation deviation of the amount of asking load, and closed-loop control is carried out to product gas requirement quality flow control valve, steam flow control valve, it is complete
Coal-burning boiler SCR flue gas denitrification system operating loads are followed into urea liquid hydrolysis ammonia system.Simultaneously in fire coal
In boiler SCR flue gas denitrification systems, discharged nitrous oxides index request when one aspect of the present invention disclosure satisfy that boiler varying duty is protected
Card hydrolysis of urea reaction system is continuous, stable operation.On the other hand urea liquid can be reduced in boiler under-capacity operation
Waste, the operation of hydrolysis of urea system high efficiency is ensured to greatest extent.
By the way that real-time detection is carried out to urea concentration to urea solution density and urea solution temperature Jing functions f3, drop
Low requirement when preparing to urea liquid to solution concentration, has saved the cost of investment of urea solution preparing device.Meanwhile,
The computational accuracy to hydrolysis product gas composition is improve, is that overall control is laid a good foundation.
Reacting ammonia amount processed to hydrolysis of urea by product gas requirement quality flow control valve and steam flow control valve is carried out
Adjust, SCR region need not again install ammonia flow regulating valve, reduce the usage amount of control device, reduce the dimension of whole system
Shield amount.
Corresponding correction factor is reserved by pair correlation function, can be according to the concrete feelings of equipment in the hot debugging of system
Condition is corrected in time, meets the operation characteristic of distinct device.Even in actual motion, it is also possible to repaiied according to operation deviation
Just, it is ensured that the flexibility of whole system.
Claims (2)
1. a kind of hydrolysis of urea reactor control method, it is characterised in that comprise the steps,
Step one, is adjusted according to ammonia requirement quality flow to product gas requirement quality flow；
1.1 by urea solution density and urea solution temperature, by urea solution density and mass concentration relation function f3, obtain
Urea solution mass concentration under corresponding temperature operating mode；
1.2, by ammonia demand and urea solution mass concentration, are needed by hydrolysis product gas requirement quality flow and ammonia
Seek mass flow relation function f1, obtain product gas requirement quality flow under correspondence urea concentration operating mode；
1.3 using product gas requirement quality flow as product throughput PID control desired value, with product gas correction factor and product
The real-time traffic of product gas together carries out closed loop product throughput PID control, realizes that product gas requirement quality flow follows ammonia to need
The direct change of the amount of asking；
Step 2, is adjusted according to ammonia demand to steam flow；
2.1 by urea solution mass concentration and product gas requirement quality flow, by hydrolysis product gas requirement quality flow
With reaction calorific requirement relation function f2, obtain reacting calorific requirement under correspondence urea solution mass concentration operating mode；
2.2 by vapor (steam) temperature and steam pressure, by saturated steam gasification latent heat function f4, obtain that steam is gasified totally works as
Front thermal discharge；And with reaction calorific requirement compare obtain heat when steam demand flow；
2.3 using steam demand flow as steam flow PID control desired value, with steam correction factor and real-time steam stream
Amount together carries out closed loop steam flow PID control, realizes that steam flow follows the direct change of ammonia demand；
Wherein, hydrolysis product gas requirement quality flow and ammonia requirement quality discharge relation function f1, it is embodied as,
QProduct gas=(QNH3×1.7647)/w；
Wherein, QProduct gasFor hydrolysis of urea reactor product demand gas mass flow；QNH3For ammonia requirement quality flow；W is that urea is molten
Liquid mass concentration；
Hydrolysis product gas requirement quality flow and reaction calorific requirement relation function f2, it is embodied as,
qInhale=A × w × QProduct gas
Wherein, qInhaleCalorific requirement is reacted for hydrolysis of urea；A is hydrolysis of urea reactor product gas requirement quality flow and reaction calorific requirement
Coefficient；QProduct gasFor hydrolysis of urea reactor product gas requirement quality flow；
Urea solution density and mass concentration relation function f3, it is embodied as,
W=2.71 × 10-3t-4.2+(7.36×10-6t2+29.72t+26.31ρ-12.12)1/2；
Wherein, urea solution temperature when t reacts for hydrolysis of urea；ρ is urea solution density；
By saturated steam gasification latent heat function f4；
When plus vapours be saturated mode when be expressed as,
qPut=4.184 × (- 0.003t2+0.139t+557.6)；
Wherein, qPutSaturation water is condensed into by unit quality saturated steam and releases heat；
When it is unsaturated state to add vapours, steam pressure is introduced into f4In be modified.
2. a kind of hydrolysis of urea reactor control system, it is characterised in that include referring to for receiving hydrolysis reactor ammonia demand
Make, the PLC of hydrolysis reactor measurement signal；
Described PLC is included such as lower module；
For according to urea solution density and urea solution temperature, by urea solution density and mass concentration relation function f3, obtain
The 3rd detection module of urea solution mass concentration under corresponding temperature operating mode；
For ammonia demand and urea solution mass concentration, by hydrolysis product gas requirement quality flow and ammonia demand
Mass flow relation function f1, obtain the first detection mould of product gas requirement quality flow under correspondence urea concentration operating mode
Block；
For using product gas requirement quality flow as product throughput PID control desired value, with product gas correction factor and
The real-time traffic of product gas together carries out the product gas pid control module of closed loop product throughput PID control；Product gas PID are controlled
The output end connection product gas requirement quality flow control valve of molding block；
For according to urea solution mass concentration and product gas requirement quality flow, by hydrolysis product gas requirement quality stream
Amount and reaction calorific requirement relation function f2, obtain reacting the detection mould of calorific requirement second under correspondence urea solution mass concentration operating mode
Block；
For according to vapor (steam) temperature and steam pressure, by saturated steam gasification latent heat function f4, obtain what steam was gasified totally
Current thermal discharge；And with reaction calorific requirement compare obtain heat when the detection module of steam demand flow the 4th；
For using steam demand flow as steam flow PID control desired value, with steam correction factor and real-time steam
Flow together carries out the steam pid control module of closed loop steam flow PID control；The output end connection of steam pid control module
Steam flow control valve；
Wherein, hydrolysis product gas requirement quality flow and ammonia requirement quality discharge relation function f1, it is embodied as,
QProduct gas=(QNH3×1.7647)/w；
Wherein, QProduct gasFor hydrolysis of urea reactor product demand gas mass flow；QNH3For ammonia requirement quality flow；W is that urea is molten
Liquid mass concentration；
Hydrolysis product gas requirement quality flow and reaction calorific requirement relation function f2, it is embodied as,
qInhale=A × w × QProduct gas
Wherein, qInhaleCalorific requirement is reacted for hydrolysis of urea；A is hydrolysis of urea reactor product gas requirement quality flow and reaction calorific requirement
Coefficient；QProduct gasFor hydrolysis of urea reactor product gas requirement quality flow；
Urea solution density and mass concentration relation function f3, it is embodied as,
W=2.71 × 10-3t-4.2+(7.36×10-6t2+29.72t+26.31ρ-12.12)1/2；
Wherein, urea solution temperature when t reacts for hydrolysis of urea；ρ is urea solution density；
By saturated steam gasification latent heat function f4；
When plus vapours be saturated mode when be expressed as,
qPut=4.184 × (- 0.003t2+0.139t+557.6)；
Wherein, qPutSaturation water is condensed into by unit quality saturated steam and releases heat；
When it is unsaturated state to add vapours, steam pressure is introduced into f4In be modified.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN110498426B (en) * | 2019-09-20 | 2021-02-26 | 中化重庆涪陵化工有限公司 | Digital online ammonia water concentration adjusting system and method |
| CN110554715A (en) * | 2019-10-25 | 2019-12-10 | 攀钢集团攀枝花钢铁研究院有限公司 | RBF neural network-based PID control method for hydrolysis process temperature of titanyl sulfate plus seed crystal |
| CN114516645A (en) * | 2020-11-19 | 2022-05-20 | 陕西青朗万城环保科技有限公司 | Method for pyrolyzing urea by microwaves and control system thereof |
| CN114560477B (en) * | 2022-03-17 | 2023-04-04 | 西安热工研究院有限公司 | Urea catalytic hydrolysis control system and method for flue gas denitration |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7220395B2 (en) * | 1997-03-21 | 2007-05-22 | Ec&C Technologies, Inc. | Methods for the production of ammonia from urea and/or biuret, and uses for NOx and/or particulate matter removal |
| CN103979575A (en) * | 2014-05-16 | 2014-08-13 | 北京博智伟德环保科技有限公司 | System and control method for producing ammonia gas by hydrolyzing urea solution |
| CN104556146A (en) * | 2014-12-22 | 2015-04-29 | 成都天化化工工程技术有限公司 | Device for rapidly responding to required ammonia amount changes in urea-hydrolysis ammonia preparation and implementation method of device |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20030211024A1 (en) * | 2002-05-10 | 2003-11-13 | Wojichowski David Lee | Methods of converting urea to ammonia for SCR, SNCR and flue gas conditioning |
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Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7220395B2 (en) * | 1997-03-21 | 2007-05-22 | Ec&C Technologies, Inc. | Methods for the production of ammonia from urea and/or biuret, and uses for NOx and/or particulate matter removal |
| CN103979575A (en) * | 2014-05-16 | 2014-08-13 | 北京博智伟德环保科技有限公司 | System and control method for producing ammonia gas by hydrolyzing urea solution |
| CN104556146A (en) * | 2014-12-22 | 2015-04-29 | 成都天化化工工程技术有限公司 | Device for rapidly responding to required ammonia amount changes in urea-hydrolysis ammonia preparation and implementation method of device |
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